Apparatus for distilling hydrocarbon oil



July 17, 1934. R. E. WILSON APPARATUS FOR DISTILLING HYDROCARBON OIL Original Filed May 16, 1928 bmw Esas mh QW MKM.

Nwm

NNN.

Ulu Il:

Patented July 17, 1934 Unirse STATES .PATENT QFFICE APPARATUS FOR DISTILLING HYDRCARBON OIL Robert E. Wilson, Chicago, Ill., assigner to Standard i! Company, Whiting, Ind., a corporation of Indiana claims. (ci. 19a- 110) This invention reates to the distillation of vhydrocarbon oils and will be readily understood from the following description illustrated by the accompanying drawing which shows diagramg matica'lly an apparatus for such distillation.

This application is a division of my co-pending application, Serial Number 278,191, filed May 16, 1928.

Referring to the drawing, a feed pipe 10, prom vided with' a pump 11, is adapted to supply crude or other oil to aseries of heat exchanging coils 12, 13, 14 and 15. These coils are provided with valves arid valved by-passes so that all or none or any desired part of the oil may be passed 1g through any one coil.

The outlet 18 from the coil 15 leads into an expansion chamber 17, which preferably is located at an intermediate point of a fractionating column 18, which has a rectifying section 19 above 2a the chamber 17 and a stripping section 20 below said chamber. From the top of said column a vapor outlet 2l leads to a suitable condenser 22.

The coil l2 is located in the upper part of the column 18 so that the feed-oil is heated by the vapors therein, and at the same time part of the vapors is condensed so as to supply re-lux to the rectiiying section 19. At its bottom the column 18 is provided with an inlet 23 for stripping steam for the stripping section 20, and also with an oil outlet 24.

The outlet 24 is heat-controlled, is provided with a pump 25 and leads into 261, 'the i'irst of a series oi pipe-still sections 261, 262, 263, 264, 265 and 266, shown as six in number, located in a suitable furnace 27, which is provided with suit`1 able iiring means 23 and flue 29. The outlets of the pipe-still sections 261, 262, 263, 264 and 265 are provided with valves 301, 302, 303, 364 and 305, and are connected to a manifold 31. This mania@ iold is provided with valves 321, 322, 323 and 324 between adjacent pairs of pipe-stili section outlets connecting thereto. -adjacent the manifold 31 is another manifold 33 to which the inlets of pipe-still sections 262, 263, 264, 265 and 266 connect, said inlets being provided with valves 342, 343, 344, 345 and 346. The manifold 33 is provided with valves 352, 353, 354 and 355 between the points of connection of the inlets of adjacent pairs o1 pipe still sections. By-passes connect the outlet of eachl section with the inlet ci the next section. Said 'oy-passes are controlled by valves 361, 362, 363, 364 and 365.

From the upper end ci the manifold 31 a pipe 37 leads into an expansion chamber 38 which is 55 preferably located at an intermediate point o fractionating column 39, which has a rectifying section 40 above the chamber 38 and a stripping section 4l below said chamber. From the top of said column a vapor outlet 42 leads to a suitable condenser 43. The coil 13 is located in the upper part of the column 39 so that the oil passing therethrough is heated by the vapors therein, and at the same time part of the vapors is condensed so as to supply reux to the rectifying section 40. At its bottom the column 39 is provided with an inlet 44 for stripping steam for the stripping section 4l and also with an oil outlet 45. The outlet 45 is float-controlled, is provided with a pump 46 and leads into the upper end of the manifold 33. 70

From the lower end of the manifold 31, a pipe 47 leads into an expansion chamber 48 which is preferably located at an intermediate .point of a fractionatng column 49, which has a rectifying section 50 above the chamber 48 and a stripping, 75 section 5l below said chamber. rom the top of said column a vapor outlet 52 leads to a suitable condenser 53. The coil 14 is located in the upper part of the column 49 so that the oil passing therethrough is heated by the vapors therein, and at the same time part of the vapors is condensed so as to supply reflux to the rectifying section 50. At its bottom the column 49 is provided with an inlet 54 for stripping steamfcr the stripping section 5l and also with an oil outlet 55. The outlet 55 is float-controlled, is provided with a pump 56 and leads into the lower end of the manifold 33. A pipe 73 leads into the pipe 55 for the purpose of supplying steam thereto.

The outlet of pipe still section 266 is connected by a pipe57 to an expansion chamber 58. Below the chamber v58 is a stripping section 59 provided with a stripping steam inlet 60 and a tar outlet 61. From the top of the chamber 53va por pipe 62 leads to an intermediate point 06;;95 iractionating column 63. From the top oi sai?.l column 63, a vapor outiet 64 leads to a suitable` condenser 65. The coil 15 is located in the upper#l part of the column 63 so that the oil passing therethrough is heated by the vapors therein, and 19@ at the same time part of the vapors is condensed so as tosupply reux for the fractionation of the vapors. At its bottom the column 63 is provided with an inlet 66 for stripping steam and also with an oil outlet 67.

If desired, the pumps 25, 46 and 56 may be replaced by oat controlled valves, in which case the vapor lines 21, 42 and 52 should be provided with suitable regulating valves 68 adapted to maintain the necessary decreasing pressures in n@ the columns 18. 39 and 49, all derived. from the feed pump 11.

The float-controls of the pumps 25, 46 and 56, or of the valves which may be substituted for said pumps should be such that they open and close very gradually for a considerable variation in the depth of oil in the bases of the columns 18, 39 and 49, thus preventing wide variations in the amount of oil passing through ihe pipe still sections 261 to 266. Any one or more of the columns may be provided, intermediate or adjacent the heat exchanger coils in the tops of the columns, with a reflux collecting pan provided with a valved outlet leading into the corresponding overhead pipe, in the manner described in my Patent No. 1,731,479, granted October 15, 1929. By way of example, the column 39 is shown provided vwith a collecting pan 69 located below the coil 13 and connected by a valved pipe 70 to the vapor line 42.

In case further cooling is necessary in any of the columns, means may be provided for pumping back distillate to the top thereof. Such means is diagrammatically shown in connection with column 63 and comprises a pump 71 and a pump back line 72 which lfeeds into the column above the top plate.

In operation, the feed oil is supplied by pump 11 through pipe 10 to the coils 12, 13, 14 and 15 in series and by pipe 16 into the expansion chamber 17 in the column 18. The temperature of the oil issuing from the pipe 16 should suitably be about 450 F. Temperature regulation is attained by diverting a part or all of the 110W through one or more of the by-passes of the coils 12, 13, 14 or 15. Such control can ordinarily he effected by by--passing coil 15 to a certain extent.

The unvaporized oil together with condensate refluxed from the fractionating section 19 passes down through the stripping section 20. Suflicient v steam is supplied by pipe 23 to deprive the descending oil of all gasoline fractions. The vapors and steam ascend through the rectifying section 19 in countcrcurrent to the reflux condensed by the coil 12, which abstracts heat from the vapors. The amount of reux may be controlled by bypassing a, part of the feed flow, if desired. The gasoline vapors pass by pipe 21 to the condenser 22 Where they are condensed.

Oil passes from the bottom of the column 18 by pipe 24 and is forced into the inlet of pipe still section 261. This oil may be caused to flow through one or more of the sections 261 to 266. For example, by closing the valves 301, 342, 322 and 362 and opening valves 302, 321 and 361, the oil is caused to pass through sections 261 and 262 and emerges by pipe 37 at a temperature of about 600 F. It then passes into the expansion chamber 38 in the column 39.

The unvaporized oil together with reflux from the rectifying section 40, passes down the stripping section 41 and is stripped with steam introduced by pipe 44 in sufficient quantity to remove all kerosene fractions therefrom. The vaporized oil and the vapors and steam from the stripping section 41 pass unwardly through the rectifying section 40 in countercurrent to the reflux condensed by the coil 13 and is thereby deprived of heavy components. The coil 13 is of sufiicient size to condense at least sufficient vapors for reflux. If more than sufficient oil is condensed a desired part may be withdrawn from the pan 69 by valved pipe 70 and passed to thev condenser 43 with the vapors from pipe 42. The column 39 is controlled to yield at condenser 43,

Locarno refined oil or kerosene. This control is eected primarily by the temperature of the oil issuing into the chamber 38 and secondarily by the amount of steam supplied by pipe 44 and the amount of reilux employed.

From the bottom of column 39 oil is forced through pipe 45 to the upper end of the inlet manifold 33 from which it is caused to now through a desired number of pipe still sections 261 to 265. For example, by closing valves 303, 305, 323, 342, 344, 353, 362 and 364 and opening valves 304, 324, 343; 352 and 363 this oil is caused to pass through the th'ird and fourth sections and to emerge through the pipe 47 which supplies it to chamber 48 of column 49 at about 700 F. This column is controlled similarly to the column 39 so as to give gas oil of desired characteristics in the condenser 53.

From the bottom of the column 49, oil together with steam admitted by pipe 73 passes by pipe 55 to the lower end of inlet manifold 33 from which it is caused to ow through a desired number of the pipe still sections 261 to 266. For example, by closing valves 305, 346, 354 and 364, and opening valves 345, 355 and 365, this oil is caused to pass through the fifth and sixth sections and to emerge through the pipe 57 which supplies it to the chamber 58 at about 750 F. In the case of Mid-Continent oil, about 3% lbs. of steam per gallon of the original crude oil may suitably be admitted by pipe 73. The unvaporized oil passes down through the stripping section 59 wherein it is treated with sufficient steam to eiect the vaporization of the desired lubricants from the tar. The tar passes out through the pipe 61. The vaporized oil together with the steam and vapors from the stripping section 59, pass by pipe 62 to an intermediate point of the column 63 and pass upwardly therethrough in countercurrent to descending reflux. This reflux may be derived from condensation of vapors by coil 15, or pump-back of distillate through line 72. The vapors of the light lubricants pass over pipe 64 to condenser 65 where they are condensed. The heavy lubricants pass from the base of the tower 63 by pipe 67. The characteristics of these lubricants are controlled by supplying an appropriate amount of steam by pipe 66.

As indicated above, the oil may be supplied to each pipe still section by separate pumps or the process can be conducted under pressure supplied by the feed pump, said pressure being caused to decrease from one column to another by interposition of Asuitable regulable automatic valves. The characteristics of the products from each column may be controlled to a certain extent by adjusting the pressure at Which it operates.

Although the present invention has been described in connection with the details of a specific embodiment thereof, it is not intended that such details shall be regarded as limitations upon the scope of the invention, except in so far as included in the accompanying claims.

What I claim as new is:

1. In an apparatus for distilling hydrocarbon oils, a plurality of fractionating columns, a pipe still comprising a plurality of sections, adjustable means for connecting any desired number of sections in series, a plurality of separate conduits adapted to supply oil from different of said columns to said still, adjusta' 'e means for selectively connecting each of said conduits to inlets of different of said sections, a plurality of conduits adapted to supply oil separately to each of said columns, and adjustable means for selectively connecting the last said conduits with outlets of diierent of said pipe still sections.

2. In an apparatus for distilling hydrocarbon oils, means for preheating oil by passing it through a series of coils in the tops of a plurality of reux fractionating columns, means for flashing said preheated oil in a fractionating tower, means for withdrawing the ashed vaporized oil from said tower, means for withdrawing and conveying the unvaporized ashed oil from said tower to a. pipe still, and means for heating said withdrawn oil to produce vaporized and unvaporized oil, said means comprising a pipe coil of selectively modifiable effective length, and means for conveying the oil which has been heated in said coil to one of the reflux fractionating columns wherein the vaporized oil is separated from the unvaporized residue, means for'withdrawing and conveying the unvaporized residue from said column and means for subjecting the withdrawn residue to further heating, said means comprising a second pipe coil of selectively modifiable elective length, and means for conveying the oil which has been heated in said second coil to another of the reux fractionating columns wherein the vaporized and condensed oil in the bottoms of said towers.

4. In an apparatus for distillingv hydrocarbon oils, a plurality of reflux fractionating columns the vapors withdrawn from each of which are independently condensed, means for withdrawing the unvaporized residue from at least the rst two columns, means for additionally heating the withdrawn residue and means for conveying at least a part of the said additionally heated residue to the next subsequent reuxfractionating column in the unit, said heating means comprising heating coils of selectively modifiable effective length.

5. An apparatus such as that dened in claim 4, in which the reflux fractionating columns are equipped with means for introducing steam into the lower portions thereof for stripping the unvaporized and condensed oil in the bottoms of said towers.

ROBERT E. WILSON. 

